Sulfur recovery apparatus



June 7, 1960 WEBB SULFUR RECOVERY APPARATUS 7 Sheets-Sheet 1 Filed May 28, 1956 CONDENSING SYSTEM N RE wN l- R CONDENSATE INVENTOR. MAURICE wees WM )WQ FIG.

ATTORNEY June 7, 1960 M. WEBB SULFUR RECOVERY APPARATUS 7 Sheets-Sheet 2 Filed May 28, 1956 INVENTOR. MAURICE WEBB Wk/ A T TOR/V5 Y June 7, 1960 WEBB 2,939,769

SULFUR RECOVERY APPARATUS Filed May 28, 1956 '7 Sheets-Sheet 3 A B *7 T 49 g 52 FIG. 3

72 4 Q @vs O O 6 L w o 0 62 so 80 o O o as FIG. 4 INVENTOR.

AURICE WEBB M kit- 7' ATTORNEY June 7, 1960 M. WEBB 2,939,769

SULFUR RECOVERY APPARATUS Filed May 2a, 1956 v Sheets-Sheet 4 F I 9 INVENTOR.

MAURICE WEBB BY 2 2 z k ATTORNEY FIG. 8

r M. WEBB SULFUR RECOVERY APPARATUS June 7, 1960 7 Sheets-Sheet. 5

Filed May 28, 1956 INVENTOR. MAURICE WEBB BYM )z/mlfl7 ATTORNEY June 7, 1960 M. WEBB SULFUR RECOVERY APPARATUS 7 Sheets-Sheet 6 Filed May 28, 1956 FIG. IO

FIG.

INVENTOR. MAURICE WEBB FIG.

ATTORNEY June 7, 1960 WEBB 2,939,769

SULFUR RECOVERY APPARATUS Filed May 28, 1956 I 7 Sheets-Sheet 7 II L 2 II I 4 IBO I76 FIG.

\ J INVENTOR.

MAURICE WEEIB United States Patent SULFUR RECOVERY APPARATUS Maurice Webb, Tulsa, Okla., assignor to Pan American Petroleum Corporation, a corporation of Delaware Filed May 28, 1956, Ser. No. 587,738

11 Claims. (Cl. 23-262) larly, it is concerned with novel equipment design which makes possible the construction of a highly eflicient and compact sulfur recovery plant.

At present two procedures are employed commercially for the recovery of free sulfur from sour gas streams. In one type of operation all of the'feed is introduced into a boiler together with sufiicient air or other source of free oxygen to oxidize one-third of the hydrogen sulfide in the feedto sulfur dioxide. As the mixture of hot gases is cooled in the furnace boiler which has a pressure tight case, some sulfur is produced and is recovered. The gaseous effluent from the boiler is then adjusted to a temperature of from about 400 to 450 F. The resulting reaction mixture is then injected into a reaction zone filled with a suitable catalyst, a substantial conversion, e.g. 75 percent, of hydrogen sulfide to free sulfur obtained,

the gaseous products then usually sent through an economizer or condenser and thereafter introduced into aliquid sulfur scrubbing unit. The unreacted gases taken off the scrubber overhead line are then adjusted to a temperature of from about 400 to 450 F. and sent to a second reaction zone. The products from this reactor are then led to a second scrubber to recover free sulfur therefrom.

Other methods of sulfur recovery involve dividing the feed stream and separately burning one-third thereof to sulfur dioxide, after whichthe latter is combined with the remaining two-thirds of the original feed gas to give a mixture roughly equivalent to that produced when all of the gas is passed through the boiler in the manner generally described above. With a process of this sort using two converters, the method of processing the stream through the system and recovering free sulfur is substantially the same as is involved when the reaction mixture is prepared by introducing allof the feed gas intoa furnace and burning one-third of said gas to sulfur dioxide. Both methods require essentially the same items of equipment, i.e. a boiler, two converters, two condensers, a gas-liquid separator for each of said condensers, two reheaters or inlinecburners, and a liquid sulfur storagepit. In addition to being quite costly, plants of this type require steam jacketed lines and considerable space which frequently is an important factor, particularly in crowded refinery areas.

Accordingly, it is an object of my invention to provide a compact sulfur recovery plant involving the use of a specially designed boiler structure which provides in the upper portion thereof separate means for condensing the product streams from the converters. It is another object of my invention to eliminate reheaters or inline burners frequently used for purposes of controlling the feed gas temperature to the converters. It is a further object of my inventionrtotconstruct the overallplant such that all process lines are self-draining, and thus eliminate the need for steam. jacketed ldraintlines. It is-another object ofrny invention. to provide. anovel separator and storagev ice tank design, the use of which eliminates the necessity for a gas-liquid separator, or equivalent thereof, for .each condenser utilized. Still another object of my invention is to provide an overall plant layout based primarily on the aforesaid novel boiler design whereby it is possible to eliminate all boiler feed water preparation facilities. For example, this latter object can be accomplished by using the produced steam in an elevated amine l'eboiler of the type employed in Girbotol sour gas sweetening units.

For a better understanding of my invention there is shownin the accompanying drawings a series of embodiments where:

Figure 1 is a front end elevational view of a sulfur recovery plant embodying my invention illustrating a particular arrangement of piping and equipment.

Figure 2 is a side elevational view of the arrangement shown in Figure l.

Figure 3 is a side elevational view of the novel boiler design.

Figure 4 is an end view of the boiler shown in Figure 3, illustrating in further detail the position of the two principal sections of the furnace, i.e. the boiler section and the condensing sections.

Figure 5 is a sectional view of the boiler shown in Figure '3.

Figure 6 is a detailed drawing of the fire tube section shown in Figure 5.

Figure 7 is a fragmentary isometric end view principally in section of the boiler of my invention having the front cover removed.

Figure 8 is a front end view of the boiler tube sheet shown in Figure3 taken along line A--A.

Figure 9 is a rear view of the boiler tube sheet shown in Figure 3 taken along line B-B.

Figure 10 is a sectional view of Figure 6 taken along line C-C.

Figure 11 is an elevational view partly in section of a novel liquid sulfur separator and storage tank.

Figure 12 is a sectional view of Figure 1.0 taken along line D--D.

Figure 13 is a fragmentary end view partly in section of the combination separator and storage tank of my invention.

Figure 14 is a plan view in section taken along line E-E of Figure 11.

Figure 15 is a plan view of the liquid sulfur separator and storage tank showing in detail a piping arrangement employed for handling gaseous and liquid product flowing to the separator and for gaseous efiluent comingfrom the separator.

Similar reference characters refer to similar parts throughout the several views of the drawings and the description.

Broadly, my invention contemplates use of a specially designed boiler in which substantially the lower half thereof comprises a main fire tube and steam tubes. In the fire tube section hydrogen sulfide is burned producing temperatures in the neighborhood of 2200* to about 2-500 F., by employing suificient air to produce a final mixture of hydrogen sulfide to sulfur dioxide in a mol ratio of about 2:1. A gas tight metal plate at each end of the boiler divides the upper and lower inter ior portions of the structure on the gas side thereof only, i.e. steam tubes in :the upper half of the unit are in contactwitli the same water that contacts the steam tubes in the lowerha-lf thereof. The gas side in the upper half of the structure at each end of the boiler is preferably divided in half by means of a gas tight metal plate or partition. This provides separate entrance areas or compartments for .the product gas from each of the two converters employed. Hot gaseous reactants are removed from the boiler sec- .tion, some produced sulfur recoveredtherefirom in a section of the liquid separator and storage tank and the remainder of said reactants sent to the first converter in accordance with the more detailed description appearing below; After reaction in the first converter the product gas is sent to that portion of the boiler designed as the condenser section to'handle said product gas from the first converter. The resulting condensate, together with uncondensed gases, is next sent to a separator. After separation of sulfur in a section of the liquid separator and storage tank to be described in greater'detail later, the uncondensed reactants are sent to the second converter and the general procedure of condensation, sulfur separation, etc., repeated with the condensation step, this time occurring in a different and separate portion of the boiler from that in which product sulfur from the first converter was condensed. Steam generated during the simultaneous oxidation of about one-third of the hydrogen sulfide to sulfur dioxide and the condensation of converter product gas as generally outlined above is withdrawn from the boiler, and, if desired, it may be sent to a unit in which steam is used as a heating medium or to a suitable elevated condenser after which the resulting condensate is returned to the water or liquid side of the boiler by gravity. In this manner boiler feed water is continuously supplied to the unit without further treatment.

My invention may be further illustrated by reference to the accompanying drawings wherein Figures 1 and 2 are front end and side elevational views, respectively, of

a' preferred arrangement of piping and equipment embodying my invention in which air is brought in through line 2 and mixed with acid (H 8) gas entering furnace 4' through line 6. The furnace is supported by means of I beams 8 which in turn restfon concrete footings 10 set in concrete pad 12. A second supporting structure holding vessel 14 comprises vertical I beams 16 resting on footings 18 also supported by concrete pad 12. Vessel 14 has two gas-tight compartments each of which contains a catalyst bed. Cross-beam 20 makes the supporting structure more rigid and transmits the weight of vessel 14 to the supporting column 16. Boiler 4 is inclined at an angle of about so that free sulfur condensed therein or produced as a result of the oxidation of one-third of the hydrogen sulfide to sulfur dioxide is removed along with the process streams from the rear portion of said boiler, as hereinafter described in detail, by means of line 22 and sent to partially submerged gas-liquid separator and storage tank 24 set in a concrete support25. Usually tank 24 is maintained at a temperature in the neighborhood of from about 250 to about 300 F. by the produced sulfur and by the hot process gas streams in order that the liquid product sulfur is kept in a pumpable and free flowing condition.

.The exposed portion of tank 24 may be covered with of the resulting mixture in line 30 subsequently going into the first catalyst chamber in vessel 14 is at the de sired initial temperature of about 450 F. Product gas from the first catalyst chamber in vessel 14 is withdravm through line 38 and sent to the first condensing section of boiler 4 via entrance port 64. Condensed product sulfur, together with unreacted product gas, is withdrawn through exit port 65 and line 42 andsent to the second separating section in tank 24. Uncondensed reactants issue from the secondseparating section through line 44 and are mixed with hot bypass gas passing from furnace 4 through three-way valve 46. The resulting mixture comprises the feed gas to the second catalyst chamber and is transmitted thereto through line 32. Hot product gas is taken from the base of the second catalyst chamber in vessel 14 through line 40 and enters the second condensing section of the boiler 4 through inlet port 82. In the upper portion of the boiler product sulfur vapors are condensed to liquid sulfur and the latter together with uncondensed gases are sent through exit port 66 (Figure 3), directly opposite exit port'65, and line 48 to storage tank 24 where said gases are separated from product liquid sulfur and vented through a stack not shown.

Steam generated in both the lower and upper sections of boiler 4 is led off through steam outlet nozzle 49' and line 50 at a pressure of about 50 pounds (absolute). This steam may be used for process heating or for a number of other purposes. For example, such steam may be conducted to a suitable condensing unit, shown diagrammatically as 51 and the resulting condensate returned to the boiler via line 53 and entrance port 80.

The overall plant structure as shown in Figures 1 and 2 with the particular equipment sizes given stands approximately 20 feet high and covers an area of about 330 square feet. The furnace itself may be 15 to 20 feet in length by 5 to 8 feet in diameter. The separator and storage tank may be .25 to 30 feet long by 6 to 8 feet in diameter., The overall length of the vessel serving as the two reactors may be from 12 to 15 feet with a diameter range of 6 to 8 feet. The capacity of a plant of this size may range from about 10 to about 25 tons of sulfur per day; I

Figures 3 and 4 are detailed elevational side and front end views, respectively, of boiler 4. Thus, in Figure 3 a manway 52 is provided for access to the steam section of the boiler. Nozzle 54 serves as a fitting for the boiler pressure reliefvalve. Hand holes 56 and 58 are provided at both ends of the base of the boiler for occasional cleaning. An exit port 60 leading from a point near the front end of the lower half of the boiler carries hot bypass gas from the furnace fire tube for purposes previously explained. An exit port 62 appears on the opposite side of furnace 4 and also handles hot bypass gas from the fire tube as previously explained. Entrance port 82 receives product gas coming from the second catalyst chamber and supplies said gas to the second condensing section of the furnace. After condensation occurs the mixture of uncondensed gases plus liquid product sulfur is withdrawn from the condensing section through exit port 66. I Figure 4 shows the front end of the furnace consisting principally of face plates 68 and 70. These plates may be secured to the boiler by bolting them to a flanged support member integral with the shell portion of said boiler.

They may also be bolted to vertical steel support 72 and horizontal member 74. Hand holes 76 and 78 serve as a means of access into the separate condensing sections of the furnace. Inlet port 80 receives condensate water and supplies it to 'the steam section of the boiler. Entrance ports 64 and 82 receive product gas from the first and second catalyst chambers, respectively, in accordance with the procedure generally set forth above and which will be described in greater detail below.

Figure 5 is a sectional view of the novel boiler design of my invention comprising a cylindrical shell 83 containing fire tube 84 into which acid gas and air flow through entrance ports 6 and 2, respectively. Surrounding the front portion of fire tube 84 is a castable refractory material 88. Fire tube 84 has a rear metal cover plate 86 protected fromthe hot combustion products by means of castable refractory 89. Combustion occurs in fire tube 84. Hot process gases produced in said tube then pass through outlets near the end of fire tube 84, one of said outlets 102 beingshown herein. Thereafter, said gases enter tubes 108 where the final cooling in the boiler section is accomplished. Portions of fire tube 84 :drot waterieoolediby tthe-steamrside of the boiler .as well lsaother portionsroffsaid boiler, such as :chamber 106,

which iareiexposed toltemperaturesiin excess of 800 .F., tire .p rdtected by casta'ble refractory 88 and 125. :Re- :tubes "1B3 :and10'4 "(shownein Figures .6 and 8.) tshouldibe so'sized that theirhot gases emerging therefrom willabe :at aastemperature' of the order of about l000 to 2000 sIfsthese-gasesiare toohot they cannot be hanridledtineaconventional three-way valve such as those indicated in Figure l, at 28 and 46. If these gases are too scold an excessi-ve quantity will :be bypassed .to maintain *desirabIe tem eratures in it-he fee'd gas to the catalyst iihambers. 'l ubes 94:.secured :to tube sheet 96 and 98 aversive hot :"product gases ttrorn the catalyst chambers, said gasesrenteringrthewboiler'through entrance ports and 82 as shown in Figure 4, and are conductedinto separately confined condensing sections 120 and 122, the latter being shown in detail in Figures 7 and 8. The sulfur vapors along with unrea'cted gases pass through tiibes '94 where 'the siilfuris transformed into a liquid tpi'dduct. The .boilerbeing inclined'atan angle of about 3 from rearlto front causes .the condensed. sulfur .in-tubes fa's-we'll as thaflintubes '1'08to1 fiOWlO the rear of the boiler into chambers 100 and 110, :respectively, where *it ijs withdrawn-along'with unreactedprocess gases :through sexitport 92audllines 42 and'48, asshownintFigure 2. The-relationship .Iof return bend tubes 10-3 and "104 -tolfire tube :84 is Eshown in Jgreater detail .in.Figure 6 i in whih oneof said'tubes,104, is'indicated to run from aspoint-near the r end oflfire .tube Hand A extend 1 back to 'uubeslreet 96. Tubes '103 and -104'are in'communica- #tion with zone 106 which in i turn leads into tubes 8 "and to the 'thre'e-wayvalve "ports 60 and 62 shown in #Eigures l and 4. r

iFire brick refractory 105 protects "cover plate68 from liot combustion "gaSBSiHiZOIIC 106. In tubes 108 additional liquid sulfur may be formed and drainslinto chamber llfl along'with unreacted gases which eventually flow out oftthe boiler through exit port 92 as previously errp'lained. 'Castable refractory 1'12, secure'd'by means of -tack welded anchors 4-13, also -placed -on the underneath sidetof steel plate 114 forming the base of chamber monaster protecting the latter from the high temperatlllCS prevailingiin lower'chamber3110. IIhe furnaceis closed at therearfilower end thereof by means of a steel wan plate I16equippewwithhandhole cover 118 so iihat aceessmaybe .had to interior portions-of the struciiture communicatingwith chamber 110. The entireim itei ior ofthe boiler coming in contact withihot acidic-gases lis preferably coated with a suitable protective material such as,-for example; sodium silicate. These areas consist f'theiiriteiiors of chambers 100,106,. and.110,.as welLas :the'two-chanrbers communicatingswith' condensing-sections i120 .and 122 .'(see' Figure 7.), one .of .said two chambers :being'shown'as121and'communicating with condensing :.tsection .12 0.

:Figure' I is a fragrnentaryiisometric end view of boiler H T-with the cover plate removed. This view indicates clearly'thestructure of.the gas'ti'ght sections at thefront ead of' the boiler. The gasttight'sections at the rearof the boiler-areformed-in-anidentical'fashion. -In-this-view vertical plate 126 is shown to project from tubes 94 to the iifront edgeofhorizontaldivider plate 124 thereby making ,apossible -.-a 1 gas :tight barrier between condensing sections a120tandF122 and forming-chambers 121 and 123 which communicatewith saidisections 120 and 122, respectively. Figure 8 is a front end view of the boiler shown in Figure 3-.taken along line 'A-A with the'cover plates 68 iand lfl'rem'oved. The upperand lower front portions of ttlie 'boiler'are: divided on thergas side only by means of 'orimntalsteel plate 124 and the upper half thereof is 'rtherdiv'ided into condensing'sections "or compartments Ieand 122by means of-gas tight'vertical steel plate 126.

"mate' flt servesto'prevenvpassage'of gas between groups iofrtuhesrM and $10.8. 'lherelativeaposition .oftreturnbend tubes 103 and 104 to fire1ube -S41and:toitubes -108.is also shown.

Figure 9 is: asectional rear view OfFigureB taken'along :line-B-BJ This view indicates the similarityi-in'structure of the gas side at the rear of the :boilersto that in the' front end thereofs'hown inFigure 8. The. lower f-POI'tiOIl-Ofithfi "boiler containing the steam tubes 108 is shown to be insulated from the condensing sections 120 and 122 Eby .means of castable refractory 112. .The :rear upper and lower portions of the boiler are likewise divided .onzthe :gassides only by means of'horizontalplatei114;and:.the upper'half thereof is further'divided'by meanszof vertical :plate 127 to form the rearportions of condensingsections 120 and'122 in a manner 'similar to the structure sintth'e front of the boiler :as showniin-Figures 7 and 8. Figure 10 is a sectional view of Figure 6 taken along .steel baflle plates 140, 142 and 175 (Figure 12) welded,

respectively, to end cover 128 and the top side of cylindrical vessel 132. Plate 140 is'made rigid by means of "horizontal channel support members 144.. Product gases along with product liquid sulfur enter compartment 138 "through port 136 where the liquid sulfur flows down through U seal pipe 146. The temperature within the entire tank is maintained generally within the range of about 250 F. to about 300 F. by means of the process gases thereby assuring free flow of liquid sulfur down through seal tube 146 and out the opposite end thereof into storage zone 148 of the tank which actually serves as athird separating section. The discharge end of tube 146 is held rigid by means of a welded spacer 150 fixed to said discharge end and to a point directly opposite said aendonthe inlet side of said tube. Uncondensed gases are Withdrawn from compartment 138 through exit port 152 and returned to the reactor for further conversion of hydrogen sulfide as previously described. An identical separator compartment 154 not shown in. Figure 11, but illustrated more in detail in Figure 12 described below, is

opposite compartment 138 and has inlet and outlet ports (not shown) similar to ports 136 and 152. After reactant gases have passed through the second catalyst chamber, theresulting product gas together with liquid sulfur are introduced into main storage zone 148 through port 156.

The opposite end of the tank is equipped with a pump well 158, which is suspended from a collar at the top of the storage tank, and extends to a level generally 2 to 4 .inches above the base of the tank. Directly below the base of the pump well is a dished head sump 162. Any

gases which have not condensed at this stage of the process .are withdrawn from the tank through exit port 164 and delivered to a suitable stack not shown. Through the use of a tank of the design just mentioned above, I am able to eliminate steam jacketed lines and costly separator and scrubbing equipment employed in plants it of-rconventional design.

Figure l2is asectional viewof'the vessel shown-in .Figure 11 taken along line.D-D illustratingtin greater detail the structure of separator compartments 138 :and 154 and therelationshipof said compartments to U bend .seal tubes1148and168. Between said U bend'tubes is a riser through which condensate is withdrawn from steam header 172. Channel support'member 144spot Welde'd-to the sides of said cylindricakshell 132 'andto base plate-140 serves'as a stifiienerforithe latter. "Partition extends from plate 142 to end cover128'to'define gas' tightcompartments 138 and 154. having inletlport 13K andexit port 155, respectively.

Figure 13 is a fragmentary isometric view,'partly in section, of combination separator andstoragetank 24. This viewillustrate s the manner in which vertical plate 175 is aifixed to horizontal plate 140 to form separating compartments 138 and 154. This figure indicates particularly the manner in which a gas tight closure may be used to maintain proper temperature during periods when the plant is not operating and process gases are not entervented to the atmosphere.

" Figure 15'' is'a plan view of separator andstorage tank 24showing the piping arrangement to and away from tank 24 when the latter is employed in combination with the boiler and reactors. shown in Figures 1 and 2. 'At the end opposite thatinto which the .productgases discharge a conduit 190 attached to exit or exhaust port 164 leads to stack 192 where unreacted product gases are Liquid product sulfur is removed from the tank through conduit 194 by means of pump 196. I

Utilization of the apparatus of my invention'in .the recovery of free sulfur by the partial oxidation of hy-' drogen sulfide in a known manner and under the'conditions set out below will be further illustrated by the fol lowing example when interpreted in light of the. foregoing drawings. a

Table Sulfur Sulfur. Removed, Feed to lstGon- 1st Con- Removed, Composition Acid Air #1 Sepa- 1st Converter denser Sepa- Gas rater verter Eflluent Etfluent rator;

Compart- Compartment meut' ing the tank to supply heat. In this system, header 176, provided with steam inlet line 178, is aflixed to lines 180 and 182 which in turn divide their flow of steam into lines 184 and'186, respectively, all of said lines 180 to 186, in-

clusive, terminating in header 172. These lines are sup- 7 ported and held free from the base of the tank by means of U rails 188. The entire steam line assembly is slanted so that the included angle defined by the base of the tank and the steam lines themselves terminating in header 172 is about to thus allowing condensate to flow into header 172 and permitting subsequent withdrawal thereof through l e 1?"- By operation of the plant designedin accordance with the present invention and under the conditions set forth in the above table, 33.75 mols per hour or 11.6 long tons of sulfur per day were obtained for a recovery of 93.5 percent.

One of the outstanding features of sulfur recovery plants designed in accordance with my inventionis their compactness and relatively low initial cost. As previously mentioned, conventionally designed sulfur plants-employing a two converter system require 10 major pieces of equipment. My design on the other hand; requires only three separate major items of equipment for atwo "ti'toflverter plant. rhus' with plants producing less than it? tons of 'sulfur per day'. I amable to construct a sulfur recoveryunit in-aceordauce with my design costing from about 251 to aboUt SO percent of the expenditure required for'conventionarplants of the same capacity.

A further fa ctor' of importance affording substantial e'conom'y in sulfur recovery plants of the type contemplated byni-y invention is-the fact that all process lines -a'ie 'sel f draining. In plants of conventional design it is necessary to steam jacket r all drain lines in order to pre- "went undesirable accumulation and subsequent solidifi- 'cation of sulfur. Such lines are expensive to install and, Tiff eourse,-are subject toplugging. The use of self-draining process' lines together with an ordinary steel storage 'tank havingadequate"external insulation and being so --eonstructed to-function as a final separator of liquid :sdlfur *from"product gases serves to reduce materially initial plant investment.

so, *in operation'of afurnace of the type generally useddn'suIfur recovery plants, feed water preparation "Taoilities suoh as 'surg'e tanks, feed pumps, level controllers, 'et c addconsiderablytotheexpense. By using an ele- Watdcondenser or elevated process unit, such as amine "reboilers; that require heating steam that is self-draining babktothe steam section of the boiler, the usual feed ""waterpurification "facilities 'canbe eliminated to provide a inexpensive and serviceable unit.

Q *Whileflmydesigu isparticularlyapplicable to sour gas *"s'ourceswhichprovide from about 5 to 25 tons of sulfur per day, it obviously may be used for the recovery of muclihighertonnag'es of sulfur with equally good results. Lilgewise,"while Phave described my invention with. par- "ticlilar referenceto its use'in' a two converter type sulfur jlplantjitisequallyapplicable to plants in which only a single converter is employed. Adaptation to the latter =type'ofplantis'readily eifected merely by making the top o'fthe'boiler'a single condensing section rather than Ttwofsuehisections Sor"c'omp'artments, said single condensirlgsebtionhavingonly oneinlet port and one exit port.

1 I'folailn:

*1." In a'n a paratusfor. producing elemental sulfur from "'a"gas"coritainin'ghydrogen sulfide, the-combination which comprises an elongated enclosed metal vessel having a =-"corribustien chamber therein, means for injection of air arid"s'aid 'ga'sintosaid chamber, conduits (1) near said opposite *end'otsaid chamber communicating with the lint'erior thereofrun'ning exteriorly of said chamber and *b ck"towardtheinlet end thereof, a first tube sheet extending from wall to Wall of said vessel holding the i'op'en etids of coriduitstl) and a. portion of said chamer near the'inlet end thereof, a second tube sheet holding "said opposite end of sai'dchamberextending from wall towall of said vessel andparallel to said first tube sheet, "edriduitsin'said vessel substantially surrounding said combustion chamber and connecting said tube sheets, a first gast ightjpai't'ition extending from said first tube sheet to the "end of said'vessel adjacent said first tube sheet and 'fiom wall'to wall of said-vessel thereby defining a first 'and' a'se'cond gas' tight-chamber, each of said chambers "thus defined being in communication with separate groups of said eonnecting conduits held by said first tube sheet, the open ends of-co'n duits (1) being in communication with 'sa'id second chamber, two outlet ports in said second chamber, a .gas tight wall extending from said first par- "titiondo the vessel wall'facing said partition and from said firsttube sheet to the end of said vessel adjacent therto to divide said first chamber into two comp-artments, an inlet port in each of said compartments, :1 secondgas tight partition extending from said second tube sheet to the end-of said vessel adjacent thereto and from wall to wall of said vessel therebydefining a third and fourth gas tight chamber, each of said chambers thus defining being in communication with separate groups of said connecting conduits-adjacent said second tube Ill sheet, a n outletport in said fourth chamber, 1 a gas tight wall extending from said second partition to the"ves's'el wall facingsaid partition and from said second tube sheet to the end of said vessel adjacent said second tube-sheet to divide said third chamber into two compartments, and an outlet port in each of said last mentioned compartments.

2. In an apparatus for producing elemental sulfur from a gas containing hydrogen sulfide, the combination which comprises an elongated enclosed metal vessel having a combustion chamber therein, separate means for injection of air and said gas into said chamber, conduits 1) near the opposite end of said chamber communicating with the interior thereof running exteriorly of' said chamber and back to the inlet end thereof, afirst tube sheet extending from wall to wall of said vessel holding the open ends of conduits (l) and a portion ofs'aid chamber near the inlet end thereof, a second tube sheet holding said opposite end of said chamber extending from wall to wall of said vessel and parallel to said first tube sheet, conduits in said vessel substantially surrounding said combustion chamber and connecting said tube sheets, a first gas tight partition extending from said first tube sheet to the end of said vessel adjacent said first tube sheet and from wall to wall of said vessel thereby defining a first and second gas tight chamber, each of said c" anthers thus defined being in communication with separate groups of said connecting conduits held by said first tube sheet, the open ends of conduits (l) beingin communication with said second chamber, two outlet ports in said second chamber, a gas tight wall at about the center of said first partition and at substantially right angles therewith extending from said first partition to the vessel wall facing said partition and from said first tube sheet toth'eend of said vessel adjacent thereto to divide said first chamber into two compamtments, an in Eat port in each-of saidcompartments, a second 'gasti'ght partition extendingfrom said second tube sheet to the and of said vessel adjacent thereto and from wall towall of said vessel thereby defininga third and a fourth gas tig t chamber, each of said third and fourth chambers in communication with separate groups of-said connectin conduits adjacent said second tube sheet, an et port in said fourth chamber, a gas tight wall at out the center of said second partition and 'atsubtially right angles therewith extending from said second partition to the vessel wall facing said partition and from said second tubesheet to the end of said vessel adjacent said second tube sheet to divide said third chamber into two compartments, and an outlet portin each of said last mentioned compartments.

3. In an apparatus for producing elemental sulfur from a gas containinghydrogen sulfide, thecombination which comprises an elongated enclosedmetal vessel having a combustion chamber therein, means for injection air and said gas into'said chamber, conduits (1) near the opposite end of said chamber communicating with the interior thereof running exteriorly of said chamber and back towardthe inlet end thereof, a first tube sheet extending from wall to wall of said vessel holding the open ends of conduits -(l) and a portion of said chamber near'the inlet end thereof, a second tube sheet holdiug said opposite end of said chamber extending from ll to wall of said vessel and parallel to said first tube sheet, conduits in said vessel substantially surrounding said combustion chamber and connecting said tube sheets, a first gas tight partition extending from said first tube sheet to "the end of said vessel adjacent said first tube sheet and from wall to wall of said vessel thereby defin a first and a second gas tight chamber, each of said 4 others thus defined being in communication with separate groups of said connecting conduits, the open end of conduits (1) being in communication withsaid second chamber, an outletportin saidsecond chamber,

an inlet port :insaid first-chamber, a second gas'tight partition extending from said second tube sheet to the end of said vessel adjacent thereto and from wall to wall of said vessel thereby defining a third and a fourth gas 'tight chamber, each of said third and fourth chambers being in communication with separate groups of said connecting conduits adjacent said second tube sheet, and an outlet port in each of said third and fourth chambers.

4. in an apparatus for producing elemental sulfur from'a gas containing hydrogen sulfide, the combination which comprises an elongated enclosed metal vessel first tube sheet, conduits in said vessel substantially surrounding said combustion chamber and connecting said tube sheets, a first gas tight partition extending from said first tube sheet to the end of said vessel adjacent said first tube sheet and from wall to wall of said vessel thereby defining a first and a second gas tight chamber, each of said chambers thus defined being in communication with separate groups of said connecting conduits held by said first tube sheet, the open ends of conduits 1) being in communication with said second chamber, two outlet ports in said second chamber, a gas tight wall extending from said first partition to the vessel Wall facing said partition and from said first tube sheet to the end of said vessel adjacent thereto to divide said first chamber into two compartments, an inlet port in each of said compartments, a second gas tight partition extending from said second tube sheet to the end of said vessel ad- ,jacent thereto and from wall to wall of said vessel thereby defining a third and a fourth gas tight chamber, each of said chambers thus defined being in communication with separate groups of said connecting conduits adjacent'said second tube sheet, an outlet port in said fourth chamber, a gas tight wall extending from said second partition to the vessel wall facing said partition and from said second tube sheet to the end of said vessel adjacent said second tube sheet to divide said third chamber into two compartments, an outlet port in each of said last mentioned compartments, a separator and storage vessel connected to said outlet port in said fourth chamber, said separator and storage vessel comprising an elongated enclosed shell having a portion thereof divided into a plurality of fluid tight compartments, an inlet and outlet port in each of said last mentioned compartments, a conduit leading from each of the latter into a common portion of said separator and storage vessel, an inlet port and an outlet port in said common portion, and means for withdrawing product liquid sulfur from said shell.

5. In an apparatus for producing elemental sulfur from a gas containing hydrogen sulfide, the combination which comprises an elongated enclosed metal vessel having a combustion chamber therein, means for injection of air and said gas into said chamber, conduits (1) near the opposite end of said chamber communicating with the interior thereof running exteniorly of said chamber and back toward the inlet end thereof, a first tube sheet extending from wall to wall of said vessel holding the open ends of conduits (1) and a portion of said chamber near the inlet end thereof, a second tube sheet holding said opposite end of said chamber extending from wall to wall of said vessel and parallel to said first tube sheet, conduits in said vessel substantially surrounding said combustion chamber and connecting said tube sheets, a

first gas tight partition extending from said first tube sheet to the end of said vessel adjacent said first tube fining a first and a second gas tight chamber, each of said chambers thus defined being in communication with separate groups of said connecting conduits held by said first tube sheet, the open ends'of conduits (1) being in communication with said second chamber, two outlet ports in said second chamber, a gas tight wall extending from said first partition to the vessel wall facing said partition and from said first tube sheet to the end of said vessel adjacent thereto to divide said first chamber into two compartments, an inlet port in each of said oompar-tments, a second gas tight partition extending from said second tube sheet to the end of said vessel adjacent thereto and from wall to wall of said vessel thereby defining a third and a fourth gas tight chamber,.each of said chambers thus defined being in communication with separate groups of said connecting conduits adjacent said second tube sheet, an outlet port in said fourth chamber, a gas tight wall extending from said second partition to the vessel wall facing said partition and from said second tube sheet to the end of said vessel adjacent said second tube sheet to divide said third chamber into two compartments, an outlet port in each of said last mentioned compartments, a separator and storage vessel conned ed to said outlet port in said fourth chamber, a separate reaction chamber connected to the inlet port in each of said compartments in said first chamber and to the outlet ports in said second chamber, and separate conduits leading from said fourth chamber and from said compantments in said third chamber to said separator aud storage vessel.

6. In a separator and storage vessel for recovering elemental sulfur from a gaseous mixture containing sulfur vapors, the combination comprising an elongated enclosed shell having a plurality of contiguous fluid tight gas separation chambers within a portion ofvsaid shell for handling liquids and vaporscontaining free sulfur, the length and diameter of each of said chambers being less than the respective dimensions of said shell, an individual inlet and outlet port in each of said chambers communicating directly with the exterior of said vessel, and a separate conduit leading from each of said chambers into a common portion of said shell, each of said conduits lying within said shell.

7. In a separator and storage vessel for recovering elemental sulfur from a gaseous mixture containing sulfur vapors, the combination comprising an elongated enclosed shell having a fluid tight gas separation chamber within a portion of said shell for handling liquids and vapors containing free sulfur, the length and diameter of said chamber being less than the respective dimensions of said shell, an individual inlet and outlet port in said chamber communicating directly with the exterior of said vessel, and a separate conduit ieading from said chamber into a common portion of said shell, said conduit lying within said shell.

8. In a separator and storage vessel for recovering elemental sulfur from a gaseous mixture containing sulfur vapors, the combination comprising an elongated'enclosed shell having two fluid tight gas separation chambers within a portion of said shell for handling liquids and vapors containing free sulfur, the length and diam eter of each of said chambers being less than the respective dimensions of said shell, an individual inlet and outlet port in each of said chambers communicating directly with the exterior of said vessel, and a separate conduit leading from each of said chambers into a common por tion of said shell, each of said conduits lying within said shell.

9. In an apparatus for producing elemental sulfur from a gas containing hydrogen sulfide, the combination which comprises an enclosed metal vessel having a combustion chamber therein, means for injection of air and said gas into said chamber, an exit port in said chamber opposite said injection means, a first heat exchange means communicating with both said exit port and the exterior of said vessel, and a second heat exchange means within said vessel superimposed on and spaced apart from said first heat exchange means and said combustion chamber, said second heat exchange means having individual inlet and outlet means communicating with the exterior of said vessel and in non-communicating relationship with said combustion chamber and said first heat exchange means, said combustion chamber and said first and second heat exchange means all being enclosed in a common heat exchange section.

10. In an apparatus for producing elemental sulfur from a gas containing hydrogen sulfide, the combination which comprises an enclosed metal vessel having a combustion chamber therein, means for injection of air and said gas into said chamber, an exit port in said chamber opposite said injection means, a first heat exchange means communicating with both said exit port and the exterior of said vessel, and a second heat exchange means within said vessel and spaced apart from said first heat exchange means and said combustion chamber, said second heat exchange means having individual inlet and outlet means communicating with the exterior of said vessel and in non-communicating relationship with said combustion chamber and said first heat exchange means, said combustion chamber and said first and second heat exchange means all being enclosed in a common heat exchange section.

11. In an apparatus for producing elemental sulfur from a gas containing hydrogen sulfide, the combination which comprises an enclosed metalvessel, said vessel having a first series of tubes arranged therein to define a boiler section, a second series of tubes in said vessel defining a separate condensing section therein having individual inlet and outlet means communicating with the exterior of said vessel but not communicating within said vessel with said first series of tubes, said condensing and boiler sections being enclosed in a common heat exchange section.

References Cited in the file of this patent UNITED STATES PATENTS 1,751,534 Taylor Mar. 25, 1930 1,790,828 McKnight Feb. 3, 1931 2,589,730 Rathkey Mar. 18, 1952 2,834,655 Chute et a1 May 13, 1955 OTHER REFERENCES 

1. IN AN APPARATUS FOR PRODUCING ELEMENTAL SULFUR FROM A GAS CONTAINING HYDROGEN SULFIDE, THE COMBINATION WHICH COMPRISES AN ELONGATED ENCLOSED METAL VESSEL HAVING A COMBUSTION CHAMBER THEREIN, MEANS FOR INJECTION OF AIR AND SAID GAS INTO SAID CHAMBER, CONDUITS (1) NEAR SAID OPPOSITE END OF SAID CHAMBER COMMUNICATING WITH THE INTERIOR THEREOF RUNNING EXTERIORLY OF SAID CHAMBER AND BACK TOWARD THE INLET END THEREOF, A FIRST TUBE SHEET EXTENDING FROM WALL TO WALL OF SAID VESSEL HOLDING THE OPEN ENDS OF CONDUITS (1) AND A PORTION OF SAID CHAMBER NEAR THE INLET END THEREOF, A SECOND TUBE SHEET HOLDING SAID OPPOSITE END OF SAID CHAMBER EXTENDING FROM WALL TO WALL OF SAID VESSEL AND PARALLEL TO SAID FIRST TUBE SHEET, CONDUITS IN SAID VESSEL SUBSTANTIALLY SURROUNDING SAID COMBUSTION CHAMBER AND CONNECTING SAID TUBE SHEETS, A FIRST GAS TIGHT PARTITION EXTENDING FROM SAID FIRST TUBE SHEET TO THE END OF SAID VESSEL ADJACENT SAID FIRST TUBE SHEET AND FROM WALL TO WALL OF SAID VESSEL THEREBY DEFINING A FIRST AND A SECOND GAS TIGHT CHAMBER, EACH OF SAID CHAMBERS THUS DEFINED BEING IN COMMUNICATION WITH SEPARATE GROUPS OF SAID CONNECTING CONDUITS HELD BY SAID FIRST TUBE SHEET, THE OPEN ENDS OF CONDUITS (1) BEING IN COMMUNICATION WITH SAID SECOND CHAMBER, TWO OUTLET PORTS IN SAID SECOND CHAMBER, A GAS TIGHT WALL EXTENDING FROM SAID FIRST PARTITION TO THE VESSEL WALL FACING SAID PARTITION AND FORM SAID FIRST TUBE SHEET TO THE END OF SAID VESSEL ADJACENT THERETO TO DIVIDE SAID FIRST CHAMBER INTO TWO COMPARTMENTS, AN INLET PORT IN EACH OF SAID COMPARTMENTS A SECOND GAS TIGHT PARTITION EXTENDING FROM SAID SECOND TUBE SHEET TO THE END OF SAID VESSEL ADJACENT THERETO AND FROM WALL TO WALL OF SAID VESSEL THEREBY DEFINING A THIRD AND FOURTH GAS TIGHT CHAMBER, EACH OF SAID CHAMBERS THUS DEFINING BEING IN COMMUNICATION WITH SEPARATE GROUPS OF SAID CONNECTING CONDUITS ADJACENT SAID SECOND TUBE SHEET, AN OUTLET PORT IN SAID FOURTH CHAMBER, A GAS TIGHT WALL EXTENDING FROM SAID SECOND PARTITION TO THE VESSEL WALL FACING SAID PARTITION AND FROM SAID SECOND TUBE SHEET TO THE END OF SAID VESSEL ADJACENT SAID SECOND TUBE SHEET TO DIVIDE SAID THIRD CHAMBER INTO TWO COMPARTMENTS, AND AN OUTLET PORT IN EACH OF SAID LAST MENTIONED COMPARTMENTS. 